Thermal swing reactor including a multi-flight auger

ABSTRACT

A thermal swing reactor including a multi-flight auger and methods for solar thermochemical reactions are disclosed. The reactor includes a multi-flight auger having different helix portions having different pitch. Embodiments of reactors include at least two distinct reactor portions between which there is at least a pressure differential. In embodiments, reactive particles are exchanged between portions during a reaction cycle to thermally reduce the particles at first conditions and oxidize the particles at second conditions to produce chemical work from heat.

CROSS-REFERENCE TO RELATED APPLICATIONS

This application claims benefit of U.S. Provisional Patent ApplicationNo. 61/823,480, “Multi-Flight Auger for Solar Thermochemical FuelProduction”, filed May 15, 2013, which is incorporated by referenceherein in its entirety.

GOVERNMENT INTERESTS

Embodiments of the invention were developed under Contract No.DE-AC04-94AL85000 between Sandia Corporation and the U.S. Department ofEnergy. The United States Government has certain rights in thisinvention.

TECHNICAL FIELD

Embodiments of the present invention relate to a material conveyor andmore particularly relates to a multi-flight auger reactor for thermalswing processing.

BACKGROUND

Solar concentration systems typically entail optics (mirrors or lenses)to focus a large area of sunlight, or solar thermal energy, onto a smallarea. The solar thermal energy may drive a heat engine, such as a steamturbine, which may be further coupled to an electrical power generatorto convert a portion of the solar thermal energy into electricity. Solarconcentration systems may also drive a thermochemical reaction togenerate a fuel that chemically stores a portion of the solar thermalenergy. Water splitting, gasification of coal, and reforming of methaneare all under investigation as potential solar thermochemical fuelproduction techniques. Solar concentration systems may drive otherimportant reactions on an industrial scale as well, such as CO₂reduction into CO, for example.

Many solar thermochemical reactions entail a redox cycle. In a watersplitting reaction to produce hydrogen from water, a metal-oxide redoxpair is thermally reduced and the reduced reactive media then drivesdecomposition of water. The metal oxide is then reduced again to repeatthe cycle. While identifying advantageous metal-oxides is currently asubject of research, thermodynamic considerations dictate the thermalreduction portion of the cycle generally requires a high temperature,typically between 1000-2000° C., depending on the reactive oxide chosenand other conditions in the system.

Solar thermochemical reactors can take many forms, affording more orless efficient fuel production, scalability, etc. One conventionalsystem utilizes a honeycomb substrate that is coated with the reactiveoxide. The honeycomb substrate is alternately exposed to collected solarenergy to heat the system and reduce the reactive oxide, and to areactant gas, such as H₂O in the case of water splitting, to generatefuel. Such a reactor is essentially a fixed bed, and as such, sufferstemperature non-uniformities and low thermal efficiency because much ofthe solar energy is expended on heating non-reactive portions of the bed(e.g., honeycomb substrate) and is ultimately rejected from the systemas waste heat, rather than utilized for fuel production. Also, with eachredox cycle, the entire system undergoes extreme thermal cycling,leading to component fatigue.

Additionally, other thermal swing process systems and methods maybenefit from more cost efficient and productive systems and methods forheating the process material.

A system which avoids many of the difficulties and efficiencylimitations associated with existing reactors would advantageouslyadvance the art of thermal swing processing, and in particular, solarthermochemical fuel production.

SUMMARY OF THE DESCRIPTION

According to an embodiment of the disclosure, an apparatus is disclosedthat includes a first reaction zone operating a first temperature; asecond reaction zone operating at a second temperature; and a particletransport component capable of moving particles from the first reactionzone to the second reaction zone. The first reaction zone includes awindow capable of receiving sunlight from a sunlight source and a hightemperature zone heated by the received sunlight. The first reactionzone further includes a first auger within a casing, and wherein thefirst auger comprises a flight that transports particles from a particlecollection zone to the high temperature zone when the casing is rotated.

According to another embodiment of the disclosure, a solar reactorsystem is disclosed that includes a solar collection system comprisingat least one mirror; and a swing reactor having an opening for receivingsunlight directed by the at least one mirror. The swing reactor includesa first reaction zone operating a first temperature; a second reactionzone operating at a second temperature; a particle transport componentcapable of moving particles from the first reaction zone to the secondreaction zone. The first reaction zone includes s a window capable ofreceiving sunlight from a sunlight source and a high temperature zoneheated by the received sunlight. The first reaction zone furtherincludes a first auger in a casing, and the first auger includes aflight that transports particles from a particle collection zone to thehigh temperature zone when the casing is rotated.

According to another embodiment of the disclosure, a method is disclosedthat includes transporting particles from a particle collection zone ata first temperature to a first reaction zone operating at a firstreaction temperature by rotating a casing surrounding an auger having aflight capable of moving the particles; transporting particles from thefirst reaction zone to a bottom portion of an inner cylinder of theauger; transporting particles to a second reaction zone operating at asecond reaction temperature less than the first reaction temperature.Heat is transferred from particles being transported from the firstreaction zone to the bottom portion of the inner cylinder of the augerto particles being transported from the particle collection zone to thefirst reaction zone. The first reaction temperature is greater than thefirst temperature; and the particles are heated to the first reactiontemperature in the first reaction zone by concentrated solar energy.

An object of the present invention is to provide a reactor that conveyssolid particulate materials between process volumes operating atdifferent temperatures while conveying solid particulate materialsbetween process volumes operating at different temperatures.

Another object of the present invention is to recover heat betweenmaterial flows.

Another object of the present invention is to increase the efficiency ofa swing reactor.

An advantage of the present invention is to increase process energyefficiency via heat recovery between process steps while conveying solidparticulate materials between process volumes operating at differenttemperatures.

Other objects, advantages and novel features, and further scope ofapplicability of the present invention will be set forth in part in thedetailed description to follow, taken in conjunction with theaccompanying drawings, and in part will become apparent to those skilledin the art upon examination of the following, or may be learned bypractice of the invention. The objects and advantages of the inventionmay be realized and attained by means of the instruments andcombinations particularly pointed out in the appended claims.

DESCRIPTION OF THE DRAWINGS

FIG. 1 shows an embodiment of a solar thermochemical system according tothe disclosure.

FIG. 2 shows a partial cut-away view of primary internal components of aswing reactor according to an embodiment of the invention.

DETAILED DESCRIPTION OF THE DISCLOSURE

Described herein are multi-flight auger reactors and methods for thermalswing, processing. Thermal swing processes include thermochemical,thermo-adsorption and other process that include changing the physicaland/or chemical properties of a material by changing processtemperature. Thermochemical systems and processes include, but are notlimited to the CO₂ and water splitting and associated fuel productionprocesses. Thermo-adsorption systems and processes include, but are notlimited to CO₂ and water capture.

In the following description, numerous details are set forth. It will beapparent, however, to one skilled in the art, that the present inventionmay be practiced without these specific details. In some instances,well-known methods and devices are shown in illustration form, ratherthan in detail, to avoid obscuring the present invention. Referencethroughout this specification to “an embodiment” means that a particularfeature, structure, function, or characteristic described in connectionwith the embodiment is included in at least one embodiment of theinvention. Thus, the appearances of the phrase “in an embodiment” invarious places throughout this specification are not necessarilyreferring to the same embodiment of the invention. Furthermore, theparticular features, structures, functions, or characteristics may becombined in any suitable manner in one or more embodiments. For example,a first embodiment may be combined with a second embodiment anywhere thetwo embodiments are not mutually exclusive.

The terms “coupled” and “connected,” along with their derivatives, maybe used herein to describe structural relationships between components.It should be understood that these terms are not intended as synonymsfor each other. Rather, in particular embodiments, “connected” may beused to indicate that two or more elements are in direct physical orelectrical contact with each other. “Coupled” my be used to indicatedthat two or more elements are in either direct or indirect (with otherintervening elements between them) physical or electrical contact witheach other, and/or that the two or more elements co-operate or interactwith each other (e.g., as in a cause and effect relationship).

FIG. 1 illustrates a thermal swing system 10 according to an embodimentof the disclosure. As can be seen in FIG. 1, the thermal swing system 10includes a thermal swing reactor 12, a component housing 14, a reactorsupport 16 and a solar collection system 18. The component housing 14includes components such as, but not limited to pumps, motors, pipingand other devices (not shown) to operate the thermal swing reactor 12.In another embodiment, one or more of the components may be housedexternal to the housing 14. In this exemplary embodiment, the componenthousing 14 is adjacent the swing reactor 12. In another embodiment, thecomponent housing 14 may be not adjacent the swing reactor, and may beco-located with or adjacent to the swing reactor 12, or may be remotelylocated, for example, on the ground or in the reactor support 16.

In this exemplary embodiment, the reactor support 16 is a cylindrical,vertical support capable of elevating the thermal swing reactor 12 andthe component housing 14. In another embodiment, the reactor support 16may be a tower or other structure capable of elevating the thermal swingreactor 12.

The solar collection system 18 includes a plurality of mirrors 20 and areflector 22. In another embodiment, the solar collection system 18 mayinclude one or more mirrors. The mirrors 20 direct solar energy to thereflector 22, where the concentrated solar energy is directed to thethermal swing reactor 12. The solar collection system 18 may includecontrol components for moving and/or positioning the mirrors 20.

FIG. 2 shows an exemplary illustration of the primary internalcomponents of the swing reactor 12 of FIG. 1 according to an embodimentof the disclosure. FIG. 2 does not show piping, conduits, such as fluidconduits, particle conduits, mechanical coupling components, seals, anddrive couplings and gears, of the swing rector 12, in order to simplifythe drawing for clarity, and as the use of these components in operationof the primary internal components would be clearly understood by one ofordinary skill in the art.

As can be seen in FIG. 2, the swing reactor 12 includes a particleheater/reduction component 24, a particle transport component 26 and anoxidation reactor component 28. The particle heater/reduction component24 may be referred to as the reduction reactor. The oxidation reactorcomponent 28 may be referred to as the oxidation reactor.

The reduction reactor 24 includes a housing 30, a casing 32 and astationary ramp device or auger 34. The housing 30 includes an aperture36 having a window 38 that allows sunlight to pass through with minimumattenuation and reach the interior 39 of the housing 30, and inparticular, to reach a top portion 40 of the auger 34.

The casing 32 is positioned within the housing 30 and around the auger34 in such a manner as to allow the casing 32 to rotate within thehousing 30 and around the auger 34. The casing 32 has a top end 42 and abottom end 44. The top end may be referred to as the high temperaturezone 42. The bottom end 44 has a particle collection zone 46. The casing32 is coupled to a drive mechanism (not shown) capable of rotating thecasing 32 within the housing 30 and around the auger 34.

The auger 34 includes a spiral ramp or flight 48 surrounding an innercylinder 49. The inner cylinder 49 includes an inner passage 51 that hasan entrance 54 and a bottom collection zone 56.

When the casing 32 is rotated, particles 50 are moved from the particlecollection zone 46 onto the flight 48 and then up the flight 48 towardsthe top end 42 of the casing 32. The particles 50 are pushed and by theforce of the rotating casing 32 moving the particles 50 towards and upthe flight 48 as the casing continues to apply force against theparticles 50. The particles 50 are pushed to the high temperature zone42, where the particles are heated by concentrated solar energy. Whenthe particles 50 reach the top of the flight 48, the particles arepushed by trailing particles into the entrance 54 of the inner passage51, where the particles proceed to fall or travel down the inner passage51 to the bottom collection zone 56 of the inner passage 51. In anembodiment, the particles undergo a reduction reaction in the hightemperature zone 42, and reduced gas products may exit the hightemperature zone 42 via an exit 57.

As the particles 50 pass down through the inner passage 51, theparticles 50 transfer heat to particles 50 being raised on the flight48. The particles 50 include the highest temperature particles 50A,second highest temperature particles 50B, third highest temperatureparticles 50C, second coolest particles 50D (these particles can be seenas the auger 34 has been partially cut away to see the inner passage51), and coolest particles 50E. It should be noted that FIG. 1 showsonly a portion of the particles 50 in order to simplify the drawing forclarity. In operation, the internal space between the casing 32 and theinner cylinder 49 may be filled with particles.

The bottom collection zone 56 has an outlet (not shown) that allowsparticles 50 to pass into a conduit 60. The conduit 60 transportsparticles 50 to the oxidation reactor 28. The oxidation reactor 28includes a housing 62 containing an oxidation zone 64. The oxidationzone 64 has an inlet 66 and an outlet 68. The inlet 66 allows for gasreactants to enter the oxidation zone 64 and be oxidized. The outlet 68allows for oxidation products to exit the oxidation zone 64.

The oxidation reactor 28 includes an oxidation reactor housing 30A and aparticle outlet 70 that allows coolest particles 50E to exit theoxidation reactor 28 and be received by the particle transport component26. In this exemplary embodiment, the particle transport component 26also has an auger configuration including a flight 71 that rotates andtransports particles 50 from an initial or low position 72 to a final orhigh position 74, where they are introduced into the particle collectionzone 46 via a cold particle inlet (not shown). A coupling to rotate theparticle transport component 26 is not shown in order to simplify thedrawing for clarity, and as the use of these components in operation ofthe primary internal components would be clearly understood by one ofordinary skill in the art.

In such a manner the particles 50 are cycled between high, reductiontemperature in the high temperature zone 42 of the oxidation reactor 28and low, oxidation temperature in the oxidation zone 64 of the oxidationreactor 28.

The reactive particles applicable to the systems and techniquesdescribed herein may generally be of any type known for thermochemicalreactions that are further suitable for conveyance by the systems andtechniques described herein. Although the reactive particles are notconsumed significantly with each reaction cycle in the exemplaryembodiments described herein, one of skill in the art will note thesystems and techniques described herein enable particle continuousaddition and are therefore readily adaptable to embodiments where thereactive particles may be consumed (e.g., volatilized) and replenished.Reactive particles applicable to the systems and techniques describedherein may be a solid media of homogenous or heterogeneous composition(e.g., carrier media coated with reactive media) and of variousporosity.

In an embodiment, the particles may be metal oxides facilitating areduction/oxidation cycle or redox cycle. These particles may metaloxides (MO_(x)s) selected from a group including, but not limited toceria (CeO₂), ferrite, manganite, cobalt oxide, and other known particlecomposition capable of similar cyclic redox reactions. Reactiveparticles applicable to the systems and techniques described herein mayalso vary in size significantly with smaller sizes having highersurface/volume ratios improving reaction rates, but potentially beingmore susceptible to sintering and/or melting. For one exemplary ceriaparticle embodiment, particle size is between about 5 μm (microns) and50 μm (microns).

The reactor may be used in concentrated solar power systems thatinclude, but are not limited to solar thermochemical hydrogen and fuelproduction, carbon dioxide and water splitting operations, water capturesuch as from air and flue gas operations, solar augmentation of fossilfuel power plants, and industrial chemical operations. Industrialchemical operations may include, but are not limited to cementmanufacture, ore thermolysis, pyrolitic production of charcoal andactivated carbon, methanol production, as well as biochar production forsoil amendment and carbon sequestration.

In an embodiment, the reactants may be CO₂ and the oxidation productsmay be CO and unreacted CO₂, and the reduction product is O₂. In thisembodiment, the particles may be oxides, such as CeO₂, ferrites,perovskites.

In an embodiment, the process may be a water capture process and thereactant may be air, and the oxidation products may be air and water,and the reduction product is water. In this embodiment, the particlesmay be a MOF or zeolite.

In an embodiment, the process may be a CO₂ capture process, and thereactant may be air and the oxidation products may be air and CO₂, andthe reduction product is CO₂. In this embodiment, the particles may besorption materials, such as zeolites or metal-organic frameworks.

The reactor design enables a high degree of solid-solid heat exchange orheat recovery in an auger used to move or circulate solid particles.Prior art particle beds are very poor thermal conductors, with acoefficient of thermal conductivity typically one to two orders ofmagnitude less than that of the constituent bulk material, andcomparable with the best insulators. It is therefore advantageous, inapplications where heat exchange between two particle beds is necessary,to minimize the relevant linear dimensions of the beds, in order tomaximize heat flow. Accordingly, the swing reactor of the presentdisclosure maximizes heat exchange between particles in differenttemperature/reactant zones by utilizing a vertical conveyor orrecilcirculator where particles are moved up a stationary auger by therotating action of the outside casing, and then discharged down throughthe hollow auger shaft.

The disclosed swing reactor utilizes an auger with a very short pitch toprovide for efficient exchange heat between the two countercurrent flowsof particles. An auger with a short pitch minimizes the transferdistance through a (highly insulating) particle bed, and maximizes heattransfer to and through the auger material itself, which is typically avastly better thermal conductor than a particle bed.

Unfortunately, a very short auger pitch hampers the conveying functionof the elevator, since conveying relies on the pressure of the particlebed to keep the particles interlocked together and moving up the augeras (roughly) one unit. In other words, an auger with a very short pitch(compared to the auger diameter) is optimal for the purposes of heatexchange, but cannot convey well or at all. Conversely, a long pitchauger (comparable to the auger diameter) is needed for efficientconveying, but is virtually useless for the purposes of heat exchange.

The multi-flight auger of the present disclosure satisfies both of theserequirements, without compromising either function. It uses multipleflights, each having an individual pitch sufficiently large to beconsistent with the need for efficient conveying. However, because thereare multiple flights (with azimuthally offset starts), the effectivedistance between flights (i.e. effective pitch) is given as theindividual pitch divided by the number of flights. This gives theeffective short pitch necessary for efficient heat exchange. The pitchof the auger is determined by the diameter, weight and surfacecharacteristics of the particles.

The operation of a multi-flight auger solid-solid heat exchanger isillustrated by again referring to FIG. 1. In this particular example,the swing reactor 12 is used to recover heat between the two flows ofparticles 50, one flow of particles 50 moving up the one or more flightsof the auger, and the second flow of particles 50 traveling down theinner passage 51 (the hotter particles traveling down the inner passage51 transferring heat to the cooler particles traveling up the flights).The auger 34 has a start 48A of the flight 48, where the particles 50are received onto the flight 48 by the pushing motion of the rotatingcasing 32. In another embodiment, the auger may have one or more flightswith corresponding flight starts. In an embodiment, the auger may havefour flights azimuthally offset by 90°. In another embodiment, the augermay have two or more flights. In an embodiment, the auger may have tenor more flights. In another embodiment, the auger may have twenty ormore flights. At the top of the auger 34, particles 50A are heated andchemically reduced by solar heat. They then move downward and near theauger inner cylinder or shaft 49, by gravity, and transfer heat (viaconduction) to the particles 50C being moved up the auger 34, havingpreviously been introduced into it via the cold particle inlet.

According to an embodiment, the aspect ratio of the flights, i.e. theratio between the effective pitch and the depth of the flights (flightoutside radius minus inside radius), is less than about 2. In practice,this means that multi-flight augers with a diameter that is largecompared to the effective pitch would have a relatively large shaft, andthe flights would occupy the periphery.

According to an embodiment of the present disclosure, the reactor may beused for a two-step metal-oxide redox cycle to produce fuel. Generally,the reactor may be conceptualized as a particle-exchange engine thatimplements a redox cycle. Reactive particles are exchanged between athermal reduction portion of the reactor where the particles are reduced(e.g., MO) at first process conditions provided during the operation,and a fuel production portion where the particles are oxidized (e.g.,MO_(x)) at second conditions during operation to produce chemical workfrom solar heating.

The thermal reduction portion thermally reduces reactive particlesthrough direct heating by solar energy to a reduction temperature T₁ anda reduction pressure P₁. At the operation, reactive particles disposedin the thermal reduction chamber are exposed to a solar energy flux. Inthe exemplary embodiment, the solar energy flux may be a beam-down anddirectly irradiates the reactive particles disposed in the thermalreduction portion through an aperture (e.g., quartz window) in theceiling of the reactor disposed a distance away from the reactiveparticles to avoid contact. However, any means known in art may beemployed to concentrate the solar energy flux to achieve a desired solarpower, such as parabolic troughs, dish, power towers, etc., andembodiments of the present invention are not limited in this respect.

For an exemplary ceria particle redox cycle, the reduction reaction ofoperation proceeds as:1/xCeO₂→1/xCeO_(2-x)+½O₂+ΔH,  (1)Where ΔH is the reduction enthalpy of ceria and x is the extent ofreduction. Other metal-oxide particles also undergo similar a reaction.

The optimal reduction temperature T₁ may vary considerably as a functionof the thermal reduction properties of the reactive particle. The extentof reduction x achieved during the operation for a particular reactiveparticle composition is also a function of the reduction pressure P₁maintained in the thermal reduction portion. Generally the reductiontemperature T₁ may be expected to be in the range of 1000° C. to 1700°C., and more particularly in the range of 1300° C. to 1600° C. for theexemplary ceria particle with the extent of reduction x increasing for agiven reduction temperature T₁ as partial pressure of oxygen in thethermal reduction portion decreases. During operation, a vacuum ispulled on the thermal reduction portion to maintain a sub-atmosphericreduction pressure P₁ and to extract oxygen (O₂) generated by thermalreduction of the reactive particles. For particular ceria particleembodiments, the reduction pressure P₁ has a partial pressure of O₂below 100 Pa, and preferably below 10 Pa, where T₁ is in the range of1300° C. to 1600° C. and preferably approximately 1500° C.

In an embodiment, the fuel production portion re-oxidizes the reducedparticles at a fuel production temperature T₂ and a fuel productionpressure P₂. During operation, reactive particles disposed in the fuelproduction portion are exposed to a reactant fluid (a gas or liquid). Inan embodiment, the reactant fluid may be steam (H₂O) for awater-splitting embodiment, or carbon dioxide (CO₂) in an alternativeembodiment. The reactive particles undergo a reaction in the presence ofthe reactant fluid and are reoxidized while the reactant fluid isreduced into fluid reaction products. Depending on the composition ofthe particle the reaction may be limited to the surface or, as in thecase of the exemplary ceria particle which is an oxygen ion conductor,the entire volume of the particle may participate in the reaction.

In an embodiment, the fluid reaction products may be hydrogen (H₂) forthe water-splitting embodiment, or CO in the alternative embodiment. Thefluid reaction products are removed from the reactor as mixed with thereactant fluid. For the exemplary ceria particle, the hydrolysisreaction of operation proceeds as:1/xCeO_(2-x)+H₂O→1/xCeO₂+H₂+ΔQ,  (2)where ΔQ is the heat released by hydrolysis and x is again the extent ofreduction. Other metal-oxide particles also undergo a similar reaction.Collection of the reaction products (e.g., H₂) separately from the O₂generated by thermal reduction is facilitated by physically separatingthe reactions (1) and (2) between the fuel production portion and thethermal reduction portion, respectively.

In advantageous embodiments, the fuel production temperature T₂ is belowthe reduction temperature T1, and in an embodiment at least 300° C.below the reduction temperature T₁, and preferably between 300° C. and600° C. below the reduction temperature T₁, to render reduction or fuelproduction thermodynamically favorable. For the exemplary watersplitting embodiment, the temperature differential between T₁ and T₂advantageously avoids a need to perform any subsequent separation of H₂from O₂. In one exemplary ceria embodiment, operation is performed at afuel production temperature T₂ of approximately 1000° C. In furtherembodiments, the fuel production pressure P₂ is maintained at a pressurehigher than the reduction pressure P₁. A higher fuel production pressureP₂ advantageously improves reactor efficiency because the rate ofreaction (2) is directly proportional to pressure. In one exemplaryceria embodiment, the fuel production pressure P₂ is at least 1 atm, andpreferably about 3-6 atm, at a point where the reactant fluid 240 (e.g.,steam) is introduced. In certain embodiments, countercurrent flow of thereactive particles and reactant fluid is provided to maximize the extentof the fuel production reaction.

With the reactor maintaining the thermal reduction portion at a thermalreduction pressure P₁ below the fuel production pressure P₂ in the fuelproduction portion during steady state operation of the reactor, thereactor may independently provide optimal processing conditions for theseparate operations of the redox cycle. For example, P₁ may be designedto achieve a greater extent of reduction x without hampering the fuelproduction half of the redox cycle.

It is to be understood that the above description is illustrative, andnot restrictive. For example, while flow diagrams in the figures show aparticular order of operations performed by certain embodiments of theinvention, it should be understood that such order is not required(e.g., alternative embodiments may perform the operations in a differentorder, combine certain operations, overlap certain operations, etc.).Furthermore, many other embodiments will be apparent to those of skillin the art upon reading and understanding the above description.Although the present invention has been described with reference tospecific exemplary embodiments, it will be recognized that the inventionis not limited to the embodiments described, but can be practiced withmodification and alteration within the spirit and scope of the appendedclaims. The scope of the invention should, therefore, be determined withreference to the appended claims, along with the full scope ofequivalents to which such claims are entitled.

What is claimed is:
 1. An apparatus, comprising: a first reaction zoneoperating at a first temperature; a second reaction zone operating at asecond temperature; a particle transport component capable of movingparticles from the first reaction zone to the second reaction zone;wherein the first reaction zone comprises a window capable of receivingsunlight from a sunlight source and a high temperature zone heated bythe received sunlight; and wherein the first reaction zone furthercomprises a first auger within a casing, and wherein the first augercomprises a flight that transports particles from a particle collectionzone to the high temperature zone when the casing is rotated.
 2. Theapparatus of claim 1, wherein the auger further comprises an innercylinder that transports particles from the high temperature zone to alower portion of the inner cylinder.
 3. The apparatus of claim 1,wherein the particle transport component comprises a second augercapable of transporting particles from the second reaction zone to theparticle collection zone when rotated.
 4. The apparatus of claim 1,further comprising: a conduit for transporting particles from a lowerportion of an inner cylinder surrounded by the flight to the secondreaction zone.
 5. The apparatus of claim 1, wherein the particles areformed of a redox reactive material.
 6. The apparatus of claim 1,wherein the first temperature is greater than 1000° C.
 7. A solarreactor system, comprising: a solar collection system comprising atleast one mirror; and a swing reactor having an opening for receivingsunlight directed by the at least one mirror; wherein the swing reactorcomprises: a first reaction zone operating at a first temperature; asecond reaction zone operating at a second temperature; a particletransport component capable of moving particles from the first reactionzone to the second reaction zone; wherein the first reaction zonecomprises a window capable of receiving sunlight from a sunlight sourceand a high temperature zone heated by the received sunlight; and whereinthe first reaction zone further comprises a first auger in a casing, andwherein the first auger comprising a flight that transports particlesfrom a particle collection zone to the high temperature zone when thecasing is rotated.
 8. The system of claim 7, wherein the auger furthercomprises an inner cylinder that transports particles from the hightemperature zone to a lower portion of the inner cylinder.
 9. The systemof claim 7, wherein the particle transport component comprises a secondauger capable of transporting particles from the second reaction zone tothe particle collection zone when rotated.
 10. The system of claim 7,further comprising: a conduit for transporting particles from a lowerportion of an inner cylinder surrounded by the flight to the secondreaction zone.
 11. The system of claim 7, wherein the particles areformed of a redox reactive material.
 12. The system of claim 7, whereinthe first temperature is greater than 1000° C.